[go: up one dir, main page]

WO2020212315A1 - Récupération d'hydrocarbures aliphatiques - Google Patents

Récupération d'hydrocarbures aliphatiques Download PDF

Info

Publication number
WO2020212315A1
WO2020212315A1 PCT/EP2020/060410 EP2020060410W WO2020212315A1 WO 2020212315 A1 WO2020212315 A1 WO 2020212315A1 EP 2020060410 W EP2020060410 W EP 2020060410W WO 2020212315 A1 WO2020212315 A1 WO 2020212315A1
Authority
WO
WIPO (PCT)
Prior art keywords
stream
organic solvent
aliphatic hydrocarbons
column
solvent
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/EP2020/060410
Other languages
English (en)
Inventor
Jean-Paul Andre Marie Joseph Ghislain LANGE
Luis Alberto GRAU LISNIER
Willem Derks
Kai Jürgen FISCHER
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Shell Internationale Research Maatschappij BV
Shell USA Inc
Original Assignee
Shell Internationale Research Maatschappij BV
Shell Oil Co
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority to EP20716851.9A priority Critical patent/EP3956421A1/fr
Priority to JP2021561687A priority patent/JP7544741B2/ja
Priority to SG11202110307RA priority patent/SG11202110307RA/en
Priority to CA3136149A priority patent/CA3136149A1/fr
Priority to US17/441,380 priority patent/US11891574B2/en
Priority to CN202080028976.3A priority patent/CN113728077A/zh
Application filed by Shell Internationale Research Maatschappij BV, Shell Oil Co filed Critical Shell Internationale Research Maatschappij BV
Priority to BR112021020625-6A priority patent/BR112021020625B1/pt
Priority to KR1020217032877A priority patent/KR102878203B1/ko
Publication of WO2020212315A1 publication Critical patent/WO2020212315A1/fr
Priority to SA521430599A priority patent/SA521430599B1/ar
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/006—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents of waste oils, e.g. PCB's containing oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/02—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents with two or more solvents, which are introduced or withdrawn separately
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/16—Oxygen-containing compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/27—Organic compounds not provided for in a single one of groups C10G21/14 - C10G21/26
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G55/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process
    • C10G55/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only
    • C10G55/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one thermal cracking step

Definitions

  • the present invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, aromatic hydrocarbons and polar components.
  • Waste plastics can be converted via pyrolysis to high- value chemicals, including olefins and aromatic hydrocarbons.
  • Pyrolysis of plastics can yield product streams having a wide boiling range, including gaseous and liquid product streams.
  • Hydrocarbons from liquid pyrolysis product streams can be cracked to produce high-value chemicals, including ethylene and propylene which are monomers that can be used in making new plastics.
  • WO2018069794 discloses a process for producing olefins and aromatic hydrocarbons from plastics wherein a liquid pyrolysis product stream is separated into a first fraction having a boiling point ⁇ 300 °C and a second fraction having a boiling point >300 °C. Only said first fraction is fed to a liquid steam cracker, whereas said second fraction is
  • hydroprocessing unit to produce a treated hydrocarbon liquid stream which is then fed to the liquid steam cracker.
  • Such hydroprocessing is also cumbersome, as it is capital
  • hydrocarbons and polar components which may originate from the pyrolysis of waste plastics, in specific mixed waste plastics. It is an object of the present invention to provide such process for the recovery of aliphatic hydrocarbons from a liquid stream comprising aliphatic hydrocarbons, aromatic hydrocarbons and polar components, which is technically advantageous, efficient and affordable, in particular a process which does not have one or more of the above- mentioned disadvantages. Such technically advantageous process would preferably result in a relatively low energy demand and/or relatively low capital expenditure.
  • Such process can be provided by contacting at least a portion of a liquid stream which comprises aliphatic hydrocarbons and additionally comprises aromatic hydrocarbons and/or polar components, with at least a portion of a first solvent stream which comprises an organic solvent, resulting in liquid- liquid extraction and in recovery of at least a portion of the aliphatic hydrocarbons.
  • a liquid hydrocarbon stream having a wide boiling range such as pyrolysis oil
  • a relatively low yield loss and feed degradation This implies that the costs of a hydrocarbon feed to a steam cracker may be reduced considerably by applying the present invention .
  • the present invention relates to a process for the recovery of aliphatic hydrocarbons from a liquid hydrocarbon feedstock stream, which comprises aliphatic hydrocarbons and additionally comprises aromatic hydrocarbons and/or polar components, said process comprising the steps of :
  • hydrocarbons and optionally organic solvent and a bottom stream from the first column comprising organic solvent and aromatic hydrocarbons and/or polar components.
  • the present invention relates to a process for steam cracking a hydrocarbon feed, wherein the hydrocarbon feed comprises aliphatic hydrocarbons recovered in the above- mentioned process of the present invention.
  • WO2018104443 discloses a method of pretreating a hydrocarbon feed
  • hydrocarbon steam cracker feed comprising contacting the feed with a solvent to produce a pretreated feed having a reduced content of fouling components that cause fouling in the preheat, convection and radiant sections of the steam cracker and a rich solvent having an increased content of fouling components.
  • hydrocarbon steam cracker feed may comprise pyrolysis oil from plastic waste.
  • the fouling components may comprise polycyclic aromatics, resins or a mixture thereof.
  • Figure 1 shows one embodiment of the process for the recovery of aliphatic hydrocarbons in accordance with the present invention.
  • Figure 2 shows another embodiment of the above-mentioned process .
  • FIG. 3 shows yet another embodiment of the above- mentioned process.
  • these components are to be selected in an overall amount not to exceed 100%.
  • substantially no in relation to the amount of a specific component in a stream, it is meant an amount which is at most 1,000, preferably at most 500, more preferably at most 100, more preferably at most 50, more preferably at most 30, more preferably at most 20, and most preferably at most 10 ppmw (parts per million by weight) of the component in question, based on the amount (i.e. weight) of said stream.
  • top stream or “bottom stream” from a column reference is made to a stream which exits the column at a position, which is between 0% and 30%, more suitably between 0% and 20%, even more suitably between 0% and 10%, based on the total column length, from the top of the column or the bottom of the column,
  • liquid hydrocarbon feedstock stream which comprises aliphatic hydrocarbons and additionally comprises aromatic hydrocarbons and/or polar components
  • the liquid hydrocarbon feedstock stream comprises both aliphatic hydrocarbons having a boiling point of from 30 to 300 °C and aliphatic hydrocarbons having a boiling point of from greater than 300 to 600 °C in a weight ratio of from 99:1 to 1:99.
  • the amount of aliphatic hydrocarbons having a boiling point of from 30 to 300 °C, based on the total amount of aliphatic hydrocarbons having a boiling point of from 30 to 600 °C, may be at most 99 wt . % or at most 80 wt . % or at most 60 wt . % or at most 40 wt . % or at most 30 wt . % or at most 20 wt . % or at most 10 wt . % .
  • the amount of aliphatic hydrocarbons having a boiling point of from 30 to 300 °C may be at least 1 wt . % or at least 5 wt . % or at least 10 wt . % or at least 20 wt . % or at least 30 wt . % .
  • the liquid hydrocarbon feedstock stream may comprise varying amounts of aliphatic hydrocarbons within a wide boiling point range of from 30 to 600 °C.
  • feedstock stream may also vary within a wide range, for example of from 5 to 50 carbon atoms.
  • feedstock stream may be at least 4 or at least 5 or at least
  • the amount of aliphatic hydrocarbons in the liquid hydrocarbon feedstock stream may be at least 30 wt . % or at least 50 wt . % or at least 80 wt . % or at least 90 wt . % or at least 95 wt . % or at least 99 wt . % and may be smaller than 100 wt . % or at most 99 wt . % or at most 90 wt . % or at most 80 wt . % or at most 70 wt . % .
  • the aliphatic hydrocarbons in the liquid hydrocarbon feedstock stream may be at least 30 wt . % or at least 50 wt . % or at least 80 wt . % or at least 90 wt . % or at least 95 wt . % or at least 99 wt . % and may be smaller than 100 wt . % or at most 99 wt . % or
  • hydrocarbons may be cyclic, linear and branched.
  • the aliphatic hydrocarbons in the liquid hydrocarbon feedstock stream may comprise non-olefinic (paraffinic) and olefinic aliphatic compounds.
  • the amount of paraffinic aliphatic compounds in the liquid hydrocarbon feedstock stream may be at least 20 wt . % or at least 40 wt . % or at least 60 wt . % or at least 80 wt . % and may be smaller than 100 wt . % or at most 99 wt . % or at most 80 wt . % or at most 60 wt . % .
  • the amount of olefinic aliphatic compounds in the liquid hydrocarbon feedstock stream may be smaller than 100 wt . % or at least 20 wt . % or at least 40 wt . % or at least 60 wt . % or at least 80 wt . % and may be at most 99 wt . % or at most 80 wt . % or at most 60 wt . % .
  • the olefinic compounds may comprise aliphatic compounds having one carbon-carbon double bond (mono-olefins) and/or aliphatic compounds having two or more carbon-carbon double bonds which latter compounds may be conjugated or non- conjugated.
  • the aliphatic compounds having two or more carbon-carbon double bonds may include compounds having double bonds at alpha and omega positions.
  • the amount of mono-olefins in the liquid hydrocarbon feedstock stream based on the total weight of the liquid hydrocarbon feedstock stream, may be at least 20 wt . % or at least 40 wt . % or at least 60 wt . % or at least 80 wt . % and may be smaller than 100 wt . % or at most 99 wt .
  • the amount of conjugated aliphatic compounds having two or more carbon-carbon double bonds in the liquid hydrocarbon feedstock stream may be greater than 0 wt . % or at least 10 wt . % or at least 20 wt . % or at least 40 wt . % or at least 60 wt . % and may be at most 80 wt . % or at most 60 wt . % or at most 40 wt . % .
  • hydrocarbon feedstock stream based on the total weight of the liquid hydrocarbon feedstock stream, may be greater than 0 wt . % or at least 5 wt . % or at least 10 wt . % or at least 15 wt . % or at least 20 wt . % or at least 25 wt . % or at least 30 wt . % and may be at most 50 wt . % or at most 40 wt . % or at most 30 wt . % or at most 20 wt . % .
  • the aromatic hydrocarbons may comprise monocyclic and/or polycyclic aromatic hydrocarbons.
  • An example of a monocyclic aromatic hydrocarbon is styrene.
  • the polycyclic aromatic hydrocarbons may comprise non-fused and/or fused polycyclic aromatic hydrocarbons.
  • An example of a non-fused polycyclic aromatic hydrocarbon is oligostyrene .
  • Styrene and oligostyrene may originate from polystyrene.
  • fused polycyclic aromatic hydrocarbons are naphthalene and anthracene.
  • the aromatic ring or rings in the aromatic hydrocarbons may be substituted by one or more hydrocarbyl groups, including alkyl groups (saturated) and alkylene groups (unsaturated) .
  • an aromatic hydrocarbon which contains one or more heteroatoms is a "polar component" as further described below .
  • the amount of polar components in the liquid hydrocarbon feedstock stream may be greater than 0 wt . % or at least 0.5 wt . % or at least 1 wt . % or at least 3 wt . % or at least 5 wt . % or at least 10 wt . % or at least 15 wt . % or at least 20 wt . % and may be at most 30 wt . % or at most 20 wt . % or at most 10 wt . % or at most 5 wt . % .
  • the polar components comprise salts and/or heteroatom containing organic compounds.
  • the salts may comprise organic and/or inorganic salts.
  • the salts may comprise ammonium, an alkali metal, an alkaline earth metal or a transition metal as the cation and a carboxylate, sulphate, phosphate or a halide as the anion.
  • the heteroatom containing organic compounds contain one or more heteroatoms, which may be oxygen, nitrogen, sulfur and/or a halogen.
  • the heteroatom containing organic compounds may comprise amines, amides, nitriles, ethers, esters and acids. Further, the heteroatom containing organic compounds may be aliphatic or aromatic. Aromatic, heteroatom containing organic compounds may comprise
  • monocyclic and/or polycyclic aromatic, heteroatom containing organic compounds examples include monocyclic aromatic, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids, amino acids
  • heteroatom containing organic compounds are terephthalic acid and benzoic acid.
  • An example of a polycyclic aromatic, heteroatom containing organic compound is oligomeric
  • PET polyethylene terephthalate
  • Terephthalic acid, benzoic acid and oligomeric PET may originate from polyethylene terephthalate .
  • liquid hydrocarbon in the present invention, the liquid hydrocarbon
  • feedstock stream may comprise a liquid product produced by the pyrolysis of plastic waste, preferably mixed plastic waste.
  • liquid product may be provided in any known way, for example by the process as disclosed in above-mentioned W02018069794.
  • liquid hydrocarbon in the present invention, the liquid hydrocarbon
  • feedstock stream is fed to a first column. Further, a first solvent stream which comprises an organic solvent is fed to the first column at a position which is higher than the position at which the liquid hydrocarbon feedstock stream is fed .
  • the weight ratio of the first solvent stream to the liquid hydrocarbon feedstock stream may be at least 0.05:1 or at least 0.2:1 or at least 0.5:1 or at least 1:1 or at least 2:1 or at least 3:1 and may be at most 5:1 or at most 3:1 or at most 2:1 or at most 1:1.
  • the temperature in the first column may be at least 0 °C or at least 20 °C or at least 30 °C or at least 40 °C or at least 50 °C and may be at most 200 °C or at most 150 °C or at most 100 °C or at most 70 °C or at most 60 °C or at most 50 °C or at most 40 °C.
  • the pressure in the first column may be at least 100 mbara or at least 500 mbara or at least 1 bara or at least 1.5 bara or at least 2 bara and may be at most 20 bara or at most 15 bara or at most 10 bara or at most 5 bara or at most 3 bara or at most 2 bara or at most 1.5 bara.
  • the temperature and pressure in the first column are preferably such that the content of the first column is in the liquid state.
  • first column may also be referred to as "first extraction column”.
  • the recovered aliphatic hydrocarbons comprise aliphatic hydrocarbons having a boiling point of from 30 to 300 °C and aliphatic
  • hydrocarbons having a boiling point of from greater than 300 to 600 °C in a weight ratio of from 99:1 to 1:99 The above description of the weight ratio of aliphatic hydrocarbons having a boiling point of from 30 to 300 °C to aliphatic hydrocarbons having a boiling point of from greater than 300 to 600 °C in relation to aliphatic hydrocarbons in the liquid hydrocarbon feedstock stream also applies to the recovered aliphatic hydrocarbons.
  • said liquid-liquid extraction results in a stream comprising recovered aliphatic
  • hydrocarbons and optionally organic solvent and a bottom stream from the first column comprising organic solvent and aromatic hydrocarbons and/or polar components.
  • the former stream comprising recovered aliphatic hydrocarbons and optionally organic solvent may also be referred to as a "raffinate stream” and the latter bottom stream may also be referred to as an "extract stream”.
  • Such raffinate stream has a reduced content of aromatic hydrocarbons, conjugated aliphatic compounds having two or more carbon-carbon double bonds, and polar components.
  • Such raffinate stream comprises no or at most 10 wt . % or at most 5 wt . % or at most 1 wt . % or substantially no aromatic
  • such raffinate stream comprises no or at most 15 wt . % or at most 10 wt . % or at most 5 wt . % or at most 1 wt . % or substantially no conjugated aliphatic
  • such raffinate stream comprises no or at most 1 wt . % or substantially no polar components.
  • the organic solvent in the first solvent stream as fed to the first column in the present process preferably has a density which is at least 3% or at least 5% or at least 8% or at least 10% or at least 15% or at least 20% and at most 50% or at most 40% or at most 35% or at most 30% higher than the density of the liquid hydrocarbon feedstock stream.
  • the organic solvent in the first solvent stream contains one or more heteroatoms, which may be oxygen, nitrogen and/or sulfur. Still further, it is preferred that said organic solvent is thermally stable at a temperature of 200 °C. Still further, said organic solvent may have a boiling point which is at least 50 °C or at least 80 °C or at least 100 °C or at least 120 °C and at most 300 °C or at most 200 °C or at most 150 °C.
  • the organic solvent in the first solvent stream may be selected from the group consisting of diols and triols, including monoethylene glycol (MEG) , monopropylene glycol (MPG) and any isomer of butanediol; glycol ethers, including oligoethylene glycols, including diethylene glycol and tetraethylene glycol, and ethers thereof, including diethylene glycol dimethylether; amides, including N- alkylpyrrolidone, wherein the alkyl group may contain 1 to 8 or 1 to 3 carbon atoms, including N-methylpyrrolidone (NMP) , and dialkyl formamide, wherein the alkyl group may contain 1 to 8 or 1 to 3 carbon atoms, including dimethyl formamide (DMF) ; dialkylsulfoxide, wherein the alkyl group may contain 1 to 8 or 1 to 3 carbon atoms, including dimethylsulfoxide (DMSO) ; sulfolane; N-formyl morph
  • the organic solvent in the first solvent stream is above-mentioned N-alkylpyrrolidone, in specific NMP, or a furan ring containing component, in specific furfural. Most preferably, said solvent is NMP.
  • An aqueous solution of a quarternary ammonium salt, in specific trioctyl methyl ammonium chloride or methyl tributyl ammonium chloride, may also be used as the organic solvent in the first solvent stream.
  • the organic solvent in the first solvent stream may have a Hansen solubility parameter distance R a , heptane with respect to heptane as determined at 25 °C of at least 10 MPa 1/2 , preferably at least 15 MPa 1/2 , and at most 30 MPa 1/2 , preferably at most 25 MPa 1/2 . Still further, the organic solvent in the first solvent stream may have a difference in Hansen solubility parameter distance R a , heptane with respect to heptane compared to Hansen solubility parameter distance
  • Ra, toluene With respect to toluene (i.e. Ra, heptane - Ra, toluene) aS determined at 25 °C of at least 1.5 MPa 1/2 , preferably at least 2 MPa 1/2 , and at most 4.5 MPa 1/2 , preferably at most 4 MPa 1/2 .
  • the organic solvent in the first solvent stream has an R a , heptane of at least 10 MPa 1/2 or at least 15 MPa 1/2 and a difference in R a , heptane compared to Ra, toluene (i.e. Ra, heptane - Ra, toluene) Of at PIO St 4.5 MPa 1/2 or at most 4 MPa 1/2 .
  • Hansen solubility parameters can be used as a means for predicting the likeliness of one component compared to another component. More specifically, each component is characterized by three Hansen parameters, each generally expressed in MPa 0 ⁇ 5 : 5 d , denoting the energy from dispersion forces between molecules; d r , denoting the energy from dipolar intermolecular forces between molecules; and 5 h , denoting the energy from hydrogen bonds between molecules.
  • HSP Hansen solubility parameter
  • R a distance in HSP space between compound 1 and compound 2
  • Hansen solubility parameters for numerous solvents can be found in, among others, CRC Handbook of Solubility Parameters and Other Cohesion Parameters Second Edition by Allan F.M. Barton, CRC press 1991; Hansen Solubility Parameters : A
  • the bottom stream from the first extraction column comprises organic solvent and aromatic hydrocarbons and/or polar components, wherein said polar components comprise salts and/or heteroatom containing organic compounds.
  • said bottom stream may comprise conjugated
  • organic solvent is recovered from said bottom stream and then advantageously recycled to the first
  • the bottom stream from the first extraction column comprises organic solvent, aromatic hydrocarbons, conjugated aliphatic compounds having two or more carbon-carbon double bonds, salts, heteroatom containing organic compounds and optionally water.
  • Said water may originate from an optional second solvent stream as further described below and/or from the first solvent stream.
  • the above-mentioned bottom stream from the first extraction column may be separated into a stream comprising aromatic hydrocarbons and conjugated aliphatic compounds having two or more carbon-carbon double bonds and a stream comprising organic solvent, salts,
  • heteroatom containing organic compounds optionally water and optionally aromatic hydrocarbons.
  • the latter separation may be performed by using a decanter.
  • water is added in addition to any water that may be present in said bottom stream from the first
  • the separated aromatic hydrocarbons and conjugated aliphatic compounds having two or more carbon-carbon double bonds may be blended with pygas and processed into fuel or used in the production of aromatic compounds. Further, they may be further separated into various fractions which may be used as a solvent.
  • the above-mentioned first separation step may be omitted in case the bottom stream from the first extraction column does not comprise aromatic hydrocarbons and conjugated aliphatic compounds having two or more carbon-carbon double bonds or in case aromatic hydrocarbons and conjugated
  • aliphatic compounds having two or more carbon-carbon double bonds are recovered in another way.
  • the bottom stream from the first extraction column does comprise aromatic hydrocarbons and conjugated aliphatic compounds having two or more carbon-carbon double bonds, it is preferred to perform the first separation step. In that way, advantageously, there is no need to separate the organic solvent from aromatic hydrocarbons in a later step, for example by means of distillation which is cumbersome and energy consuming.
  • said stream may be separated into a stream comprising water, heteroatom containing organic compounds and optionally aromatic hydrocarbons, in specific aromatic hydrocarbons having a relatively low molecular weight, and a stream comprising organic solvent and salts.
  • Water may be separated in any known way, preferably by distillation. The latter separation may be performed in a distillation column. Water may form an azeotrope with aromatic hydrocarbons, in specific aromatic hydrocarbons having a relatively low molecular weight.
  • the second separation step may be performed on that bottom stream directly.
  • a stream comprising water, heteroatom containing organic compounds and optionally aromatic hydrocarbons which may result from the second separation step may be separated into a stream comprising water and a stream comprising heteroatom containing organic compounds and optionally aromatic hydrocarbons.
  • the latter separation may be performed by using a decanter. Part of the water as separated may be sent back to a distillation column used in the second separation step as a reflux stream, whereas the other part may be recycled as part of the first solvent stream or an optional second solvent stream as further described below.
  • separation step may be separated into a stream comprising organic solvent which may be recycled to the first column as part of the first solvent stream, and a solid or slurry comprising salts which solid or slurry may be disposed of as waste.
  • the latter separation may be performed by using a filter or settler.
  • the stream comprising organic solvent and salts resulting from the second separation step may be separated into a stream comprising organic solvent which may be recycled to the first column as part of the first solvent stream, and a solid or slurry comprising salts which solid or slurry may be disposed of as waste.
  • the latter separation may be performed by using a filter or settler.
  • the stream comprising organic solvent and salts resulting from the second separation step may
  • aromatic hydrocarbons and/or heteroatom containing organic compounds additionally comprise aromatic hydrocarbons and/or heteroatom containing organic compounds, in specific aromatic
  • hydrocarbons and/or heteroatom containing organic compounds having a relatively high molecular weight.
  • the latter aromatic hydrocarbons and/or heteroatom containing organic compounds may build up in the organic solvent and may be removed therefrom before recycle to the first column, by distillation of a bleed stream which comprises the organic solvent and the latter aromatic hydrocarbons and/or
  • heteroatom containing organic compounds Alternatively, part of the organic solvent containing the latter aromatic
  • hydrocarbons and/or heteroatom containing organic compounds may be bled from the process together with the above- mentioned solid or slurry comprising salts.
  • raffinate stream also comprises organic solvent, it is preferred that organic solvent is separated from the stream comprising recovered aliphatic hydrocarbons and organic solvent and is recycled to the first column.
  • organic solvent is separated from the stream comprising recovered aliphatic hydrocarbons and organic solvent and is recycled to the first column.
  • the recovered aliphatic hydrocarbons are advantageously separated from any organic solvent in the above-mentioned raffinate stream, and the separated organic solvent is advantageously recycled to the first column.
  • Organic solvent may be separated from the above-mentioned stream comprising recovered aliphatic hydrocarbons and organic solvent in any way, including distillation,
  • the present process additionally comprises the steps of providing a second solvent stream which comprises water; contacting at least a portion of the stream comprising recovered aliphatic hydrocarbons and organic solvent with at least a portion of the second solvent stream; and removing at least a portion of the organic solvent from the stream comprising recovered aliphatic hydrocarbons and organic solvent by liquid-liquid extraction of organic solvent with water.
  • the weight ratio of organic solvent in the first solvent stream to water in the second solvent stream may be at least 0.5:1 or at least 1:1 or at least 2:1 or at least 3:1 and may be at most 10:1 or at most 5:1 or at most 3:1 or at most 2:1.
  • the first and second solvent streams are fed to the first column and the second solvent stream is fed to the first column at a position which is higher than the position at which the first solvent stream is fed, resulting in a top stream from the first column
  • the bottom stream from the first extraction column comprises organic solvent, water and aromatic
  • Organic solvent and water may be recovered from said bottom stream in a way as described above, and then advantageously be recycled to the first extraction column.
  • the stream comprising recovered aliphatic hydrocarbons and organic solvent is a top stream from the first extraction column which is fed to a second column, the second solvent stream is fed to the second column at a position which is higher than the position at which the top stream from the first extraction column comprising recovered aliphatic hydrocarbons and organic solvent is fed, resulting in a top stream from the second column comprising recovered aliphatic hydrocarbons and a bottom stream from the second column comprising water and organic solvent.
  • said “second column” may also be referred to as "second extraction column”.
  • extraction column also applies to the second extraction column .
  • the first solvent stream may comprise water in addition to organic solvent in which case the bottom stream from the first extraction column comprises organic solvent, water and aromatic hydrocarbons and/or polar components.
  • the bottom stream from the second extraction column comprising water and organic solvent may be combined with the bottom stream from the first extraction column.
  • organic solvent and water may be recovered from the bottom stream from the first extraction column or from the bottom stream from the second extraction column or from a combination of said two bottom streams in a way as described above, and then advantageously be recycled to the first and second extraction columns .
  • aliphatic hydrocarbons recovered in the present process as described above may be fed to a steam cracker without a further pre-treatment, such as treatment with hydrogen
  • hydrotreating or hydroprocessing as disclosed in above- mentioned WO2018069794.
  • aliphatic hydrocarbons recovered in the present process as described above may also advantageously be separated into different fractions which each may find a different application, such as diesel, marine fuel, solvent, etc .
  • the present invention also relates to a process for steam cracking a hydrocarbon feed, wherein the hydrocarbon feed comprises aliphatic hydrocarbons recovered in a process as described above. Further, accordingly, the present invention also relates to a process for steam
  • hydrocarbon feed comprises aliphatic hydrocarbons recovered in the preceding step.
  • the hydrocarbon feed to the steam cracking process may also comprise hydrocarbons from another source, other than the present process for the recovery of aliphatic
  • hydrocarbons from a liquid hydrocarbon feedstock stream may be naphtha, hydrowax or a combination thereof .
  • the liquid hydrocarbon feedstock stream comprises aromatic hydrocarbons, polar components, conjugated aliphatic compounds having two or more carbon-carbon double bonds, or a combination thereof, these have already been removed by the present process as described above before feeding recovered hydrocarbons to a steam cracking process.
  • said removed compounds and components, especially polycyclic aromatics can no longer cause fouling in the preheat, convection and radiant sections of a steam cracker and in the downstream heat exchange and/or separation equipment for a steam cracker, for example in transfer line exchangers (TLEs) which are used to rapidly cool the effluent from a steam cracker.
  • TLEs transfer line exchangers
  • the steam cracking may be performed in any known way.
  • the hydrocarbon feed is typically preheated.
  • the feed can be heated using heat exchangers, a furnace or any other
  • the feed is steam cracked in a cracking zone under cracking conditions to produce at least olefins (including ethylene) and
  • the cracking zone may comprise any cracking system known in the art that is suitable for cracking the feed.
  • the cracking zone may comprise one or more furnaces, each
  • the cracking is performed at elevated temperatures, preferably in the range of from 650 to 1000 °C, more
  • a cracker effluent is obtained that may comprise aromatics (as produced in the steam cracking process), olefins, hydrogen, water, carbon dioxide and other hydrocarbon compounds.
  • aromatics as produced in the steam cracking process
  • olefins hydrogen, water, carbon dioxide and other hydrocarbon compounds.
  • the specific products obtained depend on the composition of the feed, the hydrocarbon-to-steam ratio, and the cracking temperature and furnace residence time.
  • the cracked products from the steam cracker are then passed through one or more heat exchangers, often referred to as TLEs ("transfer line exchangers") , to rapidly reduce the temperature of the cracked products.
  • the TLEs preferably cool the cracked products to a temperature in the range of from 400 to 550 °C.
  • feedstock stream 1 which comprises aliphatic hydrocarbons (including conjugated aliphatic compounds having two or more carbon-carbon double bonds, which are hereinafter referred to as "dienes”) , aromatic hydrocarbons, salts and heteroatom containing organic compounds; a first solvent stream 2 which comprises an organic solvent (for example N- methylpyrrolidone ) ; and a second solvent stream 3 which comprises water are fed to a first extraction column 4.
  • liquid hydrocarbon feedstock stream 1 is contacted with at least a portion of first solvent stream 2 (organic solvent) , thereby recovering at least a portion of the aliphatic hydrocarbons by liquid- liquid extraction of dienes, aromatic hydrocarbons, salts and heteroatom containing organic compounds with the organic solvent, resulting in a stream comprising recovered aliphatic hydrocarbons and organic solvent.
  • first solvent stream 2 organic solvent
  • second solvent stream 3 water
  • a stream 5 comprising recovered aliphatic hydrocarbons exits column 4 at the top.
  • a stream 6 comprising organic solvent, water, dienes, aromatic hydrocarbons, salts and heteroatom containing organic
  • Stream 6 is fed to a distillation column 7, where it is separated into a top stream 8 comprising water, dienes, aromatic hydrocarbons and heteroatom containing organic compounds and a bottom stream 9 comprising organic solvent and salts.
  • Stream 8 is fed to an overhead decanter 17, wherein it is separated into a stream 18 comprising dienes, aromatic hydrocarbons and heteroatom containing organic compounds and a stream comprising water, part of which water stream (stream 19a) is sent back to distillation column 7 as a reflux stream whereas the other part (stream 19b) is recycled (not shown) as part of second solvent stream 3.
  • Stream 9 is fed to a filter 10, where it is separated into a stream 11 comprising organic solvent and a slurry 12 comprising salts. Stream 11 is recycled (not shown) as part of first solvent stream 2.
  • feedstock stream 1 which comprises aliphatic hydrocarbons (including conjugated aliphatic compounds having two or more carbon-carbon double bonds, which are hereinafter referred to as "dienes”) , aromatic hydrocarbons, salts and heteroatom containing organic compounds; a first solvent stream 2 which comprises an organic solvent (for example N- methylpyrrolidone ) ; and a second solvent stream 3 which comprises water are fed to a first extraction column 4.
  • liquid hydrocarbon feedstock stream 1 is contacted with at least a portion of first solvent stream 2 (organic solvent) , thereby recovering a portion of the aliphatic hydrocarbons by liquid-liquid extraction of dienes, aromatic hydrocarbons, salts and heteroatom containing organic compounds with the organic solvent, resulting in a stream comprising recovered aliphatic hydrocarbons and organic solvent.
  • first solvent stream 2 organic solvent
  • second solvent stream 3 water
  • a stream 5 comprising recovered aliphatic hydrocarbons exits column 4 at the top.
  • a stream 6 comprising organic solvent, water, dienes, aromatic hydrocarbons, salts and heteroatom containing organic
  • Stream 6 is fed to a decanter 13, to which a stream 14 comprising additional water is also fed.
  • the combined streams 6 and 14 are separated into a stream 15 comprising dienes and aromatic hydrocarbons and a stream 16 comprising organic solvent, water, dienes, aromatic hydrocarbons, salts and heteroatom containing organic compounds.
  • Stream 16 is fed to a distillation column 7. In respect of the treatment in
  • feedstock stream 1 which comprises aliphatic hydrocarbons (including conjugated aliphatic compounds having two or more carbon-carbon double bonds, which are hereinafter referred to as "dienes”) , aromatic hydrocarbons, salts and heteroatom containing organic compounds; and a first solvent stream 2 which comprises an organic solvent (for example N- methylpyrrolidone ) and water are fed to a first extraction column 4a.
  • first extraction column 4a At least a portion of liquid
  • hydrocarbon feedstock stream 1 is contacted with at least a portion of first solvent stream 2 (organic solvent and water) , thereby recovering a portion of the aliphatic
  • hydrocarbons by liquid-liquid extraction of dienes, aromatic hydrocarbons, salts and heteroatom containing organic
  • a top stream 5a comprising recovered aliphatic hydrocarbons and organic solvent and a bottom stream 6 comprising organic solvent, water, dienes, aromatic hydrocarbons, salts and heteroatom containing organic compounds.
  • Stream 5a and a second solvent stream 3 which comprises water are fed to a second extraction column 4b.
  • column 4b at least a portion of stream 5a is contacted with at least a portion of second solvent stream 3 (water) , thereby removing at least a portion of the organic solvent by liquid-liquid extraction of organic solvent with water.
  • a stream 5b comprising recovered aliphatic
  • hydrocarbons exits column 4b at the top. Further, a stream 14 comprising organic solvent and water exits column 4b at the bottom. Streams 6 and 14 are fed to a decanter 13. In respect of the treatment in decanter 13 and further, downstream treatments in the process of Figure 3 reference is made to the above description of the corresponding treatments in the process of Figure 2.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé de récupération d'hydrocarbures aliphatiques à partir d'un flux de charge d'hydrocarbures liquides, qui comprend des hydrocarbures aliphatiques et comprend en outre des hydrocarbures aromatiques et/ou des composants polaires. Ledit procédé comprend les étapes consistant à : introduire le flux de charge d'hydrocarbures liquides dans une première colonne ; introduire un premier flux de solvant qui comprend un solvant organique dans la première colonne à une position qui est supérieure à la position à laquelle le flux de charge d'hydrocarbures liquides est introduit ; mettre en contact au moins une partie du flux de charge d'hydrocarbures liquides avec au moins une partie du premier flux de solvant ; et récupérer au moins une partie des hydrocarbures aliphatiques par extraction liquide-liquide d'hydrocarbures aromatiques et/ou de composants polaires avec un solvant organique. Grâce à ce procédé, un flux comprenant des hydrocarbures aliphatiques récupérés et éventuellement un solvant organique et un flux de fond provenant de la première colonne comprenant un solvant organique et des hydrocarbures aromatiques et/ou des composants polaires sont obtenus.
PCT/EP2020/060410 2019-04-18 2020-04-14 Récupération d'hydrocarbures aliphatiques Ceased WO2020212315A1 (fr)

Priority Applications (9)

Application Number Priority Date Filing Date Title
JP2021561687A JP7544741B2 (ja) 2019-04-18 2020-04-14 脂肪族炭化水素の回収
SG11202110307RA SG11202110307RA (en) 2019-04-18 2020-04-14 Recovery of aliphatic hydrocarbons
CA3136149A CA3136149A1 (fr) 2019-04-18 2020-04-14 Recuperation d'hydrocarbures aliphatiques
US17/441,380 US11891574B2 (en) 2019-04-18 2020-04-14 Recovery of aliphatic hydrocarbons
CN202080028976.3A CN113728077A (zh) 2019-04-18 2020-04-14 脂族烃的回收
EP20716851.9A EP3956421A1 (fr) 2019-04-18 2020-04-14 Récupération d'hydrocarbures aliphatiques
BR112021020625-6A BR112021020625B1 (pt) 2019-04-18 2020-04-14 Processo para craqueamento a vapor de uma alimentação de hidrocarboneto
KR1020217032877A KR102878203B1 (ko) 2019-04-18 2020-04-14 지방족 탄화수소의 회수
SA521430599A SA521430599B1 (ar) 2019-04-18 2021-10-14 استخلاص هيدروكربونات أليفاتية

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19170263.8 2019-04-18
EP19170263 2019-04-18

Publications (1)

Publication Number Publication Date
WO2020212315A1 true WO2020212315A1 (fr) 2020-10-22

Family

ID=66239903

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2020/060410 Ceased WO2020212315A1 (fr) 2019-04-18 2020-04-14 Récupération d'hydrocarbures aliphatiques

Country Status (10)

Country Link
US (1) US11891574B2 (fr)
EP (1) EP3956421A1 (fr)
JP (1) JP7544741B2 (fr)
KR (1) KR102878203B1 (fr)
CN (1) CN113728077A (fr)
AR (1) AR118708A1 (fr)
CA (1) CA3136149A1 (fr)
SA (1) SA521430599B1 (fr)
SG (1) SG11202110307RA (fr)
WO (1) WO2020212315A1 (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2022101394A1 (fr) 2020-11-13 2022-05-19 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques
WO2022101392A1 (fr) 2020-11-13 2022-05-19 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques
EP4036191A1 (fr) 2021-01-28 2022-08-03 Shell Internationale Research Maatschappij B.V. Procédé d'évacuation de contaminants à partir d'un matériau organique recyclé ou renouvelable
WO2022162298A1 (fr) 2021-01-29 2022-08-04 Totalenergies Raffinage Chimie Procede de purification d'une huile de pyrolyse en vue de sa valorisation par vapocraquage
FR3119398A1 (fr) 2021-01-29 2022-08-05 Total Raffinage Chimie Procede de purification d’une huile de pyrolyse en vue de sa valorisation par vapocraquage
WO2023066739A1 (fr) * 2021-10-18 2023-04-27 Shell Internationale Research Maatschappij B.V. Procédé de production d'huile de pyrolyse à partir de déchets plastiques
WO2024073345A1 (fr) * 2022-09-30 2024-04-04 Uop Llc Procédés et appareils de séparation d'hydrocarbures aromatiques et non aromatiques
US11959026B2 (en) 2019-03-07 2024-04-16 Refiniti Limited Process of upgrading a pyrolysis oil and upgrading solution used therein
US11999920B2 (en) 2020-09-14 2024-06-04 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock
US12031097B2 (en) 2021-10-14 2024-07-09 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks
US12304888B2 (en) 2021-03-10 2025-05-20 Ecolab Usa Inc. Stabilizer additives for plastic-derived synthetic feedstock
US12503663B2 (en) 2024-04-26 2025-12-23 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2025125033A1 (fr) * 2023-12-13 2025-06-19 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2600184A (en) * 1951-11-27 1952-06-10 Texas Co Refining kerosenes and gas oil by ternary azeotropic distillation
US3864245A (en) * 1973-11-23 1975-02-04 Universal Oil Prod Co Solvent extraction with increased polar hydrocarbon purity
CA2214305A1 (fr) * 1997-08-29 1999-02-28 Doug Hutchins Procede pour la separation d'hydrocarbures aromatiques d'une charge d'alimentation melangee
US20160369190A1 (en) * 2013-07-02 2016-12-22 Andrew Mark Ward Method of producing aromatics and light olefins from a hydrocarbon feedstock
WO2018069794A1 (fr) 2016-10-11 2018-04-19 Sabic Global Technologies, B.V. Maximisation de produits chimiques à valeur élevée à partir de plastique mixte à l'aide de différentes configurations de vapocraqueur
WO2018104443A1 (fr) 2016-12-08 2018-06-14 Shell Internationale Research Maatschappij B.V. Procédé de prétraitement et de conversion d'hydrocarbures
US20180355256A1 (en) * 2015-11-23 2018-12-13 Integrated Green Energy Singapore Pte Ltd Production of hydrocarbon fuels from plastics

Family Cites Families (50)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR1600622A (fr) 1968-05-10 1970-07-27
JPS4928642B1 (fr) 1970-04-03 1974-07-29
GB1554767A (en) 1975-08-25 1979-10-31 Exxon Research Engineering Co Thermol recovery of n-methyl-2-pyrrolidone from solutions of mixtures with reduced loss thereof
US4048062A (en) * 1976-04-22 1977-09-13 Uop Inc. Aromatic extraction with solvent recovery and regeneration
GB2040306A (en) 1978-12-29 1980-08-28 Rtl Contactor Holding Sa Removing aromatics from gas oils
US4353794A (en) 1980-11-26 1982-10-12 Uop Inc. Process for the solvent extraction of aromatics and the recovery of an aromatics-free non-aromatic product from a hydrocarbon feedstock
US4764256A (en) 1983-12-07 1988-08-16 Electric Power Research Institute, Inc. Removal of polychlorinated biphenyls by solvent extraction
CA1246483A (fr) 1985-01-04 1988-12-13 Paulino Forte Separation des composantes aromatiques et non aromatiques des charges mixtes d'hydrocarbures
AU6394886A (en) * 1985-11-01 1987-05-07 Mobil Oil Corp. Hydrocarbon solvent extraction process
US4992210A (en) 1989-03-09 1991-02-12 Betz Laboratories, Inc. Crude oil desalting process
US5114566A (en) 1989-03-09 1992-05-19 Betz Laboratories, Inc. Crude oil desalting process
US5041206A (en) * 1989-11-20 1991-08-20 Texaco Inc. Solvent extraction of lubricating oils
DE69323125T2 (de) 1992-06-29 1999-08-19 Mortimer Technology Holdings Ltd. Verfahren zur Umwandlung von Polymeren
EP0710270B1 (fr) 1993-07-20 1997-01-02 Basf Aktiengesellschaft Procede de recyclage de matieres plastiques dans un vapocraqueur
US5399244A (en) * 1993-12-06 1995-03-21 Glitsch, Inc. Process to recover benzene from mixed hydrocarbons by extractive distillation
EP0697455B1 (fr) 1994-07-22 2001-09-19 Shell Internationale Research Maatschappij B.V. Procédé de préparation d'une cire hydrogénée
US6565742B1 (en) * 1997-09-03 2003-05-20 Gtc Technology Inc. Aromatics separation process and method of retrofitting existing equipment for same
GB9902518D0 (en) 1999-02-04 1999-03-24 Bp Exploration Operating A process for deacidifying a crude oil system
US6497813B2 (en) 2001-01-19 2002-12-24 Process Dynamics, Inc. Solvent extraction refining of petroleum products
EP1581600A1 (fr) * 2002-12-27 2005-10-05 Council Of Scientific And Industrial Research Procede d'extraction d'hydrocarbures aromatiques a partir de flux petroliers
US20080194900A1 (en) 2004-12-10 2008-08-14 Bhirud Vasant L Steam Cracking with Naphtha Dearomatization
WO2008027131A1 (fr) 2006-08-31 2008-03-06 Exxonmobil Chemical Patents Inc. Disposition de goudron de vapocraquage
US8343336B2 (en) 2007-10-30 2013-01-01 Saudi Arabian Oil Company Desulfurization of whole crude oil by solvent extraction and hydrotreating
CN102216425B (zh) 2008-12-18 2014-05-14 国际壳牌研究有限公司 用于移除沥青质颗粒的方法
DE102009003044A1 (de) 2009-05-12 2010-11-18 Wacker Chemie Ag Verfahren zur Dosierung von Massen auf der Basis von Organopolysiloxanen
US8246811B2 (en) 2009-05-26 2012-08-21 IFP Energies Nouvelles Process for the production of a hydrocarbon fraction with a high octane number and a low sulfur content
US8608951B2 (en) 2009-12-30 2013-12-17 Uop Llc Process for removing metals from crude oil
US20130153394A1 (en) 2010-07-26 2013-06-20 Emil A.J. Wieser-linhart Facility and Method for Production Fuels from Biomass/Plastic Mixtures
US20120024750A1 (en) 2010-07-30 2012-02-02 Chevron U.S.A. Inc. Hydrodechlorination of ionic liquid-derived hydrocarbon products
US8551328B2 (en) 2011-01-20 2013-10-08 Basf Corporation Organic chloride adsorbent
US8795515B2 (en) 2011-06-28 2014-08-05 Chevron U.S.A. Inc. Catalytic dechlorination processes to upgrade feedstock containing chloride as fuels
US9382486B2 (en) 2012-01-27 2016-07-05 Saudi Arabian Oil Company Integrated hydrotreating, solvent deasphalting and steam pyrolysis process for direct processing of a crude oil
US9440947B2 (en) * 2012-02-26 2016-09-13 Amt International, Inc. Regeneration of selective solvents for extractive processes
US9781747B2 (en) 2013-01-29 2017-10-03 Lg Electronics Inc. Method and apparatus for transmitting random access channel designed for transmission in high carrier frequency in a wireless communication system
US20140336427A1 (en) 2013-05-09 2014-11-13 Uop Llc Methods of and apparatuses for upgrading a hydrocarbon stream including a deoxygenated pyrolysis product
US9839897B2 (en) 2013-05-30 2017-12-12 Chevron U.S.A. Inc. Method for reducing organic halide contamination in hydrocarbon products using a metal chloride
EP3017018B1 (fr) 2013-07-02 2018-09-19 Saudi Basic Industries Corporation Procédé et installation pour la conversion de pétrole brut en produits pétrochimiques présentant un meilleur rendement en btx
CN103571537B (zh) 2013-11-19 2016-05-04 广西大学 一种脱蜡溶剂及其使用方法
US8961780B1 (en) 2013-12-16 2015-02-24 Saudi Arabian Oil Company Methods for recovering organic heteroatom compounds from hydrocarbon feedstocks
WO2017083018A1 (fr) 2015-11-13 2017-05-18 Sabic Global Technologies B.V. Procédé catalytique pour réduire la teneur en chlorure d'un flux d'alimentation hydrocarboné
ES2807525T3 (es) 2015-11-30 2021-02-23 Sabic Global Technologies Bv Procedimiento de producción de materia prima de alta calidad para un proceso de craqueo con vapor
WO2017167948A1 (fr) 2016-03-31 2017-10-05 Solvay Sa Procédé de conversion de plastique en cires par craquage et mélange d'hydrocarbures ainsi obtenu
EP3408354B1 (fr) 2016-03-31 2022-08-10 Trifol Resources Limited Procédé de préparation d'une huile de base lubrifiante comprenant la décomposition thermique sélective d'un polymère de polyoléfine plastique
JP6999646B2 (ja) 2016-08-01 2022-01-18 サビック グローバル テクノロジーズ ベスローテン フェンノートシャップ 混合プラスチックの熱分解と熱分解油の脱塩素と同時に行う触媒プロセス
US10513661B2 (en) 2016-09-22 2019-12-24 Sabic Global Technologies B.V. Integrated process configuration involving the steps of pyrolysis, hydrocracking, hydrodealkylation and steam cracking
WO2018127813A1 (fr) * 2017-01-05 2018-07-12 Sabic Global Technologies, B.V. Conversion de déchets plastiques en propylène et cumène
CN106833719A (zh) 2017-03-08 2017-06-13 中国石油大学(北京) 一种萃取分离原油的方法
JP2022530180A (ja) 2019-04-23 2022-06-28 ピーティーティー グローバル ケミカル パブリック カンパニー リミテッド 有機塩化物化合物を液体炭化水素から分離するための吸着剤およびそのプロセス
FR3103822B1 (fr) 2019-12-02 2022-07-01 Ifp Energies Now Procede de traitement d’huiles de pyrolyse de plastiques en vue de leur valorisation dans une unite de vapocraquage
EP3907267A1 (fr) 2020-05-08 2021-11-10 Basf Se Procédé de purification d'une huile de pyrolyse brute provenant de la pyrolyse de déchets plastiques

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2600184A (en) * 1951-11-27 1952-06-10 Texas Co Refining kerosenes and gas oil by ternary azeotropic distillation
US3864245A (en) * 1973-11-23 1975-02-04 Universal Oil Prod Co Solvent extraction with increased polar hydrocarbon purity
CA2214305A1 (fr) * 1997-08-29 1999-02-28 Doug Hutchins Procede pour la separation d'hydrocarbures aromatiques d'une charge d'alimentation melangee
US20160369190A1 (en) * 2013-07-02 2016-12-22 Andrew Mark Ward Method of producing aromatics and light olefins from a hydrocarbon feedstock
US20180355256A1 (en) * 2015-11-23 2018-12-13 Integrated Green Energy Singapore Pte Ltd Production of hydrocarbon fuels from plastics
WO2018069794A1 (fr) 2016-10-11 2018-04-19 Sabic Global Technologies, B.V. Maximisation de produits chimiques à valeur élevée à partir de plastique mixte à l'aide de différentes configurations de vapocraqueur
WO2018104443A1 (fr) 2016-12-08 2018-06-14 Shell Internationale Research Maatschappij B.V. Procédé de prétraitement et de conversion d'hydrocarbures

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
ALLAN F.M. BARTON: "CRC Handbook of Solubility Parameters and Other Cohesion Parameters", 1991, CRC PRESS
CHARLES M. HANSEN: "Hansen Solubility Parameters: A User's Handbook", 2007, CRC PRESS
See also references of EP3956421A1

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US12492347B2 (en) 2019-03-07 2025-12-09 Refiniti Limited Process of upgrading a pyrolysis oil and upgrading solution used therein
US11959026B2 (en) 2019-03-07 2024-04-16 Refiniti Limited Process of upgrading a pyrolysis oil and upgrading solution used therein
US11999920B2 (en) 2020-09-14 2024-06-04 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock
CN116529342A (zh) * 2020-11-13 2023-08-01 国际壳牌研究有限公司 脂族烃的回收
WO2022101392A1 (fr) 2020-11-13 2022-05-19 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques
WO2022101394A1 (fr) 2020-11-13 2022-05-19 Shell Internationale Research Maatschappij B.V. Récupération d'hydrocarbures aliphatiques
EP4036191A1 (fr) 2021-01-28 2022-08-03 Shell Internationale Research Maatschappij B.V. Procédé d'évacuation de contaminants à partir d'un matériau organique recyclé ou renouvelable
WO2022162298A1 (fr) 2021-01-29 2022-08-04 Totalenergies Raffinage Chimie Procede de purification d'une huile de pyrolyse en vue de sa valorisation par vapocraquage
FR3119399A1 (fr) 2021-01-29 2022-08-05 Total Raffinage Chimie Procede de purification d’une huile de pyrolyse en vue de sa valorisation par vapocraquage
FR3119398A1 (fr) 2021-01-29 2022-08-05 Total Raffinage Chimie Procede de purification d’une huile de pyrolyse en vue de sa valorisation par vapocraquage
US12304888B2 (en) 2021-03-10 2025-05-20 Ecolab Usa Inc. Stabilizer additives for plastic-derived synthetic feedstock
US12031097B2 (en) 2021-10-14 2024-07-09 Ecolab Usa Inc. Antifouling agents for plastic-derived synthetic feedstocks
WO2023066739A1 (fr) * 2021-10-18 2023-04-27 Shell Internationale Research Maatschappij B.V. Procédé de production d'huile de pyrolyse à partir de déchets plastiques
WO2024073345A1 (fr) * 2022-09-30 2024-04-04 Uop Llc Procédés et appareils de séparation d'hydrocarbures aromatiques et non aromatiques
US12503663B2 (en) 2024-04-26 2025-12-23 Ecolab Usa Inc. Cold flow additives for plastic-derived synthetic feedstock

Also Published As

Publication number Publication date
US20220177786A1 (en) 2022-06-09
US11891574B2 (en) 2024-02-06
SA521430599B1 (ar) 2025-04-07
SG11202110307RA (en) 2021-11-29
AR118708A1 (es) 2021-10-27
EP3956421A1 (fr) 2022-02-23
BR112021020625A2 (pt) 2021-12-21
CA3136149A1 (fr) 2020-10-22
CN113728077A (zh) 2021-11-30
JP7544741B2 (ja) 2024-09-03
KR102878203B1 (ko) 2025-10-30
JP2022529946A (ja) 2022-06-27
KR20210154152A (ko) 2021-12-20

Similar Documents

Publication Publication Date Title
US11891574B2 (en) Recovery of aliphatic hydrocarbons
US9505678B2 (en) Process to produce aromatics from crude oil
US12473505B2 (en) Recovery of aliphatic hydrocarbons
CN114746532A (zh) 脂族烃的回收
KR20120030382A (ko) 부타디엔의 분별 추출
US20230374402A1 (en) Recovery of aliphatic hydrocarbons
US3103485A (en) Temperature
KR20160015248A (ko) 열분해 가솔린으로부터 ｃ5 디올레핀을 분리하는 방법 및 장치
CN112552951A (zh) 一种适用于低含量芳烃直馏石脑油中芳烃脱除的复合萃取剂及其应用方法
US12391889B2 (en) Recovery of aliphatic hydrocarbons
WO2025125033A1 (fr) Récupération d'hydrocarbures aliphatiques
BR112021020625B1 (pt) Processo para craqueamento a vapor de uma alimentação de hidrocarboneto
WO2024224119A1 (fr) Vapocraquage d'hydrocarbures liquides non hydrotraités
RU2027737C1 (ru) Способ получения сырья для малоактивного технического углерода

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 20716851

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 3136149

Country of ref document: CA

ENP Entry into the national phase

Ref document number: 2021561687

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 112021020625

Country of ref document: BR

WWE Wipo information: entry into national phase

Ref document number: 2020716851

Country of ref document: EP

ENP Entry into the national phase

Ref document number: 2020716851

Country of ref document: EP

Effective date: 20211118

ENP Entry into the national phase

Ref document number: 112021020625

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20211014

WWE Wipo information: entry into national phase

Ref document number: 521430599

Country of ref document: SA

WWE Wipo information: entry into national phase

Ref document number: 521430599

Country of ref document: SA

WWG Wipo information: grant in national office

Ref document number: 521430599

Country of ref document: SA

WWG Wipo information: grant in national office

Ref document number: 202147047397

Country of ref document: IN